A product separation method and apparatus for olefin production from syngas or CO2

Abstract

The application provides a product separation method and device for preparing olefins from synthesis gas or CO2, wherein the device comprises a first condensation unit, a variable-diameter unit and a packing unit which are sequentially communicated, and a second condensation unit which surrounds the packing unit; the packing unit is arranged between the two condensation units, high-temperature product gas is first condensed in the first condensation unit; the condensed liquid generated by condensation passes through the variable-diameter unit and enters the packing unit, the temperature of the condensed liquid entering the packing unit is further lowered due to the low temperature of the second condensation unit; meanwhile, a small amount of high-temperature product gas directly enters the packing unit through a second product gas feeding pipe, and rectification is generated between the high-temperature product gas and the low-temperature condensed liquid under the action of the temperature difference, so that the easily liquefied organic components in the condensed liquid are continuously stripped, the organic components in the condensed liquid are greatly reduced, the easily liquefied organic components in the condensed liquid are maximally recovered, and the treatment difficulty of the remaining waste water is reduced.

Description

Technical Field

[0001] This invention relates to the fields of chemical manufacturing equipment and clean coal chemical technology, and in particular to a product separation method and apparatus for the preparation of olefins from syngas or CO2. Background Technology

[0002] Olefins are among the most important chemical raw materials, providing the foundation for the synthesis of various plastics, fibers, and medical devices. China's current ethylene and propylene production both exceed 50 million tons per year, and C4 olefin production exceeds 6 million tons per year. The remaining C5 to C12 high-carbon olefins can be used to prepare various high-performance polyethylene copolymers, detergents, and fine chemical products, forming a vast chemical and materials product network. Currently, most olefins are still obtained through the cracking of petroleum feedstocks. Other developing routes include coal-to-methanol olefin production and ethane dehydrogenation-to-ethylene production. The bottleneck of the petroleum route lies in its resource dependence. The coal-to-methanol olefin production route is lengthy, requires large equipment investments, and has high carbon emissions.

[0003] The direct production of olefins from syngas or CO2 is an emerging technological route. Since syngas can be derived from coal chemical, natural gas chemical, or biomass chemical processes, this route has strong vitality and market adaptability. Undoubtedly, the catalyst is the most crucial element in the direct production of olefins from syngas. Currently, catalysts exist in the form of metal oxides coupled with molecular sieves, as well as metal carbide catalysts. However, due to the complexity of the synthesis process, the product gas always includes large amounts of CO, H2, CO2, and C1-C... 20 The presence of organic matter complicates the separation process. For example, pressurized cooling of the product gas for gas-liquid separation helps maintain the pressure head, making subsequent olefin and alkane separation more economical. However, pressurized cooling tends to dissolve more easily liquefied organic matter into the water, resulting in material loss and increased difficulty in wastewater treatment. Summary of the Invention

[0004] In view of the above-mentioned problems in the prior art, the present invention provides a product separation method and apparatus for the preparation of olefins from syngas or CO2, so as to accurately control the maximum separation of water and organic matter in the product gas of the direct preparation of olefins from syngas or CO2, and improve the recovery rate of hydrocarbons in the product gas.

[0005] The specific details of the invention are as follows:

[0006] In a first aspect, the present invention provides a product separation device for the preparation of olefins from syngas or CO2, the device comprising a primary condensation unit, a variable diameter unit and a packing unit connected in sequence, and a secondary condensation unit surrounding the packing unit.

[0007] The primary condensation unit includes a first product gas inlet pipe, a second product gas inlet pipe, and a partition baffle; wherein, the lower end of the first product gas inlet pipe is located in the primary condensation unit, the lower end of the second product gas inlet pipe is located in the packing unit, and the lower end of the partition baffle is located in the area between the lower ends of the first and second product gas inlet pipes, with both the first and second product gas inlet pipes located on the same side of the partition baffle.

[0008] Optionally, the primary condensation unit controls the temperature of the condensation zone to be between 50-85°C by setting a first heat exchanger;

[0009] The secondary condensation unit controls the temperature of the condensation zone between 0-25℃ by setting a second heat exchanger.

[0010] Optionally, the temperature of the primary condensing unit and the secondary condensing unit is controlled by circulating cooling water.

[0011] Optionally, the porosity of the packing unit is 80%-95%.

[0012] Optionally, the bottom of the secondary condensation unit is provided with a liquid outlet for receiving the remaining condensate flowing out of the packing unit and discharging it from the separation device.

[0013] Optionally, the top of the primary condensation unit is also provided with a gas outlet, which is located on the other side of the partition baffle.

[0014] Optionally, the amount of product gas entering the first product gas inlet pipe is 2-10 times that of the second product gas inlet pipe.

[0015] Secondly, the present invention provides a product separation method for the preparation of olefins from syngas or CO2, the method being applicable to the product separation apparatus for the preparation of olefins from syngas or CO2 described in the first aspect above, the method comprising the following steps:

[0016] Step 1: Control the condensation zone temperature of the primary condensing unit to 50-85℃, and control the condensation zone temperature of the secondary condensing unit to 0-25℃;

[0017] Step 2: Product gas with a volume ratio of 2-10:1 is introduced into the first product gas inlet pipe and the second product gas inlet pipe respectively. The product gas introduced into the first product gas inlet pipe is condensed in the first-stage condensation unit to form condensate liquid. The condensate liquid enters the packing unit through the diameter reducing unit.

[0018] Step 3: The temperature of the packing unit's cylinder wall is affected by the low temperature of the secondary condensation unit, and the temperature of the condensate entering it becomes even lower. It comes into contact with the product gas introduced through the second product gas feed pipe, and under the action of the temperature difference, the easily liquefied organic matter in the condensate is continuously separated and gas-lifted. The gaseous substances obtained by gas lifting are blocked by the baffle plate and return to the primary condensation unit, and exit the separation device through the gas outlet. The remaining condensate flows to the secondary condensation unit and is discharged from the separation device from the liquid outlet at the bottom of the secondary condensation unit.

[0019] The product gases include CO, H2, CO2, and Cl-C. 20 Organic matter;

[0020] The temperature of the product gas is 100-350℃.

[0021] Optionally, in step 1, controlling the condensation zone temperature of the primary condensing unit to be 50-85°C includes: introducing circulating cooling water into the first heat exchanger to control the condensation zone temperature of the primary condensing unit to be 50-85°C.

[0022] Controlling the condensation zone temperature of the secondary condensing unit to 0-25℃ includes: introducing circulating cooling water into the second heat exchanger to control the condensation zone temperature of the secondary condensing unit to 0-25℃.

[0023] Optionally, the packing unit is a plastic packing unit, a metal wire mesh packing unit, or a ceramic packing unit, with a porosity of 80%-95%.

[0024] Compared with the prior art, the present invention has the following advantages:

[0025] This invention provides a product separation method and apparatus for the preparation of olefins from syngas or CO2. The apparatus includes a primary condensation unit, a variable diameter unit, and a packing unit connected in sequence, and a secondary condensation unit surrounding the packing unit. The lower end of the first product gas feed pipe is located in the primary condensation unit, the lower end of the second product gas feed pipe is located in the packing unit, and the lower end of a partition baffle is located in the region between the lower ends of the first and second product gas feed pipes. Both the first and second product gas feed pipes are located on the same side of the partition baffle. By adding a packing unit between the two condensation units, the high-temperature product gas is first cooled to 50-85°C in the primary condensation unit. A large amount of CO2, H2, CO, and C1-C7 components in the product gas remain in gaseous form and are discharged from the separation device through the gas outlet of the primary condensation unit. The condensate produced during condensation (mainly composed of water and C4-C7 components) is cooled to 50-85°C in the primary condensation unit. 20The liquid enters the packing unit through the reducing unit. Influenced by the low temperature (0-25℃) of the secondary condensation unit, the temperature of the condensate entering the packing unit further decreases. Simultaneously, a small amount of high-temperature product gas enters the packing unit through the second product gas inlet pipe. Under the influence of the temperature difference, a distillation effect occurs between the small amount of high-temperature product gas and the low-temperature condensate, causing the easily liquefiable organic components in the condensate to be continuously stripped. The gaseous substances obtained by stripping are returned to the primary condensation unit under the obstruction of the baffle plates and exit the separation device through the gas outlet, thereby reducing the organic components (C4-C4) in the condensate. 20 The amount of condensate is greatly reduced, and the remaining condensate (mainly water) flows from the packing unit to the secondary condensation unit and is discharged from the separation unit through the liquid outlet at the bottom. Using this device and method, easily liquefiable organic components in the condensate can be recovered to the maximum extent, the water content in the gas formed during the separation process can be reduced, and the difficulty of wastewater treatment can be decreased. It has the advantages of low cost, easy scale-up, and continuous operation. Attached Figure Description

[0026] To more clearly illustrate the technical solutions in the embodiments of the present invention or the prior art, the drawings used in the description of the embodiments or the prior art will be briefly introduced below. Obviously, the drawings described below are only some embodiments of the present invention. For those skilled in the art, other drawings can be obtained based on these drawings without creative effort.

[0027] Figure 1 This invention provides a schematic diagram of the structure of a product separation device for olefin production from syngas or CO2, as shown in an embodiment of the invention.

[0028] Figure 2 A flowchart of a product separation method for preparing olefins from syngas or CO2, provided by an embodiment of the present invention, is shown.

[0029] Explanation of reference numerals in the attached figures:

[0030] 1. Primary condensing unit; 2. Variable diameter unit; 3. Packing unit; 4. Secondary condensing unit; 5. Dividing baffle; 6. First heat exchanger; 7. Second heat exchanger; 8. First product gas inlet pipe; 9. Second product gas inlet pipe; 10. Gas outlet; 11. Liquid outlet. Detailed Implementation

[0031] The technical solutions of the embodiments of the present invention will be clearly and completely described below with reference to the accompanying drawings. Obviously, the described embodiments are only some embodiments of the present invention, and not all embodiments. The following description of at least one exemplary embodiment is merely illustrative and is in no way intended to limit the present invention or its application or use. Based on the embodiments of the present invention, any product that is the same as or similar to the present invention, derived by any person under the guidance of the present invention or by combining the features of the present invention with other prior art, falls within the protection scope of the present invention. Furthermore, all other embodiments obtained by those skilled in the art without inventive effort are within the protection scope of the present invention.

[0032] Specific experimental steps or conditions are not specified in the embodiments; they can be performed according to the conventional experimental steps or conditions described in the prior art. Reagents and other instruments used, unless otherwise specified, are all commercially available conventional reagent products. Furthermore, the accompanying drawings are merely illustrative diagrams of the embodiments of the present invention and are not necessarily drawn to scale. The same reference numerals in the drawings denote the same or similar parts, and therefore, repeated descriptions of them will be omitted. Some block diagrams shown in the drawings are functional entities and do not necessarily correspond to physically or logically independent entities.

[0033] Techniques, methods, and devices known to those skilled in the art may not be discussed in detail, but where appropriate, such techniques, methods, and devices should be considered part of this specification.

[0034] In the description of this invention, it should be understood that the use of terms such as "first" and "second" to define components is merely for the purpose of distinguishing the corresponding components. Unless otherwise stated, the above terms have no special meaning and therefore should not be construed as limiting the scope of protection of this invention.

[0035] Furthermore, the technical features involved in the different embodiments of the present invention described below can be combined with each other as long as they do not conflict with each other.

[0036] This invention, focusing on maximizing the separation and recovery of easily liquefiable organic components from product gas (product gas obtained from syngas or CO2 olefin production) and reducing the water content of the recovered gas, provides a product separation device for syngas or CO2 olefin production and a product separation method suitable for this device. This reduces the amount of organic components in the condensate formed after the product gas undergoes condensation and liquefaction, thereby reducing the difficulty of post-treatment of the condensate (wastewater). It offers advantages such as low cost, easy scale-up, and continuous operation. Specific implementation details are as follows:

[0037] In a first aspect, the present invention provides a product separation device for the preparation of olefins from syngas or CO2. Figure 1 A schematic diagram of the structure of a product separation device for olefin production from syngas or CO2 provided in an embodiment of the present invention is shown, as follows: Figure 1 As shown, the device includes a primary condensation unit 1, a variable diameter unit 2, and a packing unit 3 connected in sequence, as well as a secondary condensation unit 4 surrounding the packing unit.

[0038] The primary condensation unit 1 is equipped with a first product gas inlet pipe 8, a second product gas inlet pipe 9, and a partition baffle 5. The lower end of the first product gas inlet pipe 8 is located in the primary condensation unit 1, the lower end of the second product gas inlet pipe 9 is located in the packing unit 3, and the lower end of the partition baffle 5 is located in the area between the lower ends of the first product gas inlet pipe 8 and the second product gas inlet pipe 9. The first product gas inlet pipe 8 and the second product gas inlet pipe 9 are both located on the same side of the partition baffle 5.

[0039] In specific implementation, the separation device provided in this embodiment of the invention is used to separate the product gas obtained from the direct preparation of olefins using syngas or CO2 as raw material. The product gas contains CO, H2, CO2, and C1-C2. 20 The product gas, containing organic matter, has a temperature of 100-350℃. This invention adds a packing unit 3 between two condensation units. The high-temperature product gas is first cooled to 50-85℃ in the first-stage condensation unit 1. During this process, a large amount of CO2, H2, CO, and C1-C7 components in the product gas remain in gaseous form and are discharged from the separation device through the gas outlet 10 of the first-stage condensation unit 1. The condensate produced during condensation (mainly composed of water and C4-C7 components)... 20 The condensate entering the packing unit 3 is collected through the variable diameter unit 2. Affected by the low temperature (0-25℃) of the secondary condensation unit 4, the temperature of the condensate entering the packing unit 3 is further reduced. Simultaneously, a small amount of high-temperature product gas directly enters the packing unit 3 through the second product gas feed pipe 9. Under the influence of the temperature difference, a distillation effect occurs between the small amount of high-temperature product gas and the low-temperature condensate, causing the easily liquefiable organic components in the condensate to be continuously stripped. The gaseous substances obtained from the stripping are returned to the primary condensation unit 1 under the obstruction of the baffle plate 5, and exit the separation device through the gas outlet 10, thereby reducing the organic components (C4-C4) in the condensate. 20The amount of condensate (mainly water) is greatly reduced, and the remaining condensate flows from the packing unit 3 to the secondary condensation unit 4, and is discharged from the separation device through the liquid outlet 11 at the bottom. Using this device, easily liquefiable organic components in the condensate can be recovered to the maximum extent, and the water content in the gas formed during the separation process can be reduced, as well as the difficulty of wastewater treatment. It has the advantages of low cost, easy scale-up, and continuous operation. The baffle 5 is installed in the primary condensation unit 1 to separate the inlet and outlet spaces, ensuring that the product gas inlet and outlet do not interfere with each other. It also ensures that the gaseous substances obtained by gas stripping can smoothly enter the space on the side where the gas outlet 10 of the primary condensation unit 1 is located.

[0040] See also Figure 1 The primary condensing unit 1 controls the temperature of the condensing zone between 50-85℃ by setting a first heat exchanger 6. Specifically, the temperature is controlled by continuously circulating cooling water into the first heat exchanger 6. The secondary condensing unit 2 controls the temperature of the condensing zone between 0-25℃ by setting a second heat exchanger 7. Specifically, the temperature is controlled by continuously circulating cooling water into the second heat exchanger 7.

[0041] In some implementations, distillation stripping can be achieved by introducing a small amount of product gas into the second product gas feed pipe 9, and the amount of product gas introduced into the first product gas feed pipe 8 is 2-10 times that of the second product gas feed pipe 9.

[0042] Secondly, the present invention provides a product separation method for the preparation of olefins from syngas or CO2. Figure 2 A flow chart of a product separation method for preparing olefins from syngas or CO2, provided by an embodiment of the present invention, is shown, as follows: Figure 2 As shown, this method is applicable to the product separation apparatus for olefin production from syngas or CO2 described in the first aspect above, and specifically includes the following steps:

[0043] Step 1: Control the condensation zone temperature of the primary condensing unit to 50-85℃, and control the condensation zone temperature of the secondary condensing unit to 0-25℃;

[0044] Step 2: Product gas with a volume ratio of 2-10:1 is introduced into the first product gas inlet pipe and the second product gas inlet pipe respectively. The product gas introduced into the first product gas inlet pipe is condensed in the first-stage condensation unit to form condensate liquid. The condensate liquid enters the packing unit through the diameter reducing unit.

[0045] Step 3: The temperature of the packing unit's cylinder wall is affected by the low temperature of the secondary condensation unit, causing the temperature of the condensate entering it to drop further. It comes into contact with the product gas introduced through the second product gas feed pipe, and under the action of the temperature difference, the easily liquefied organic matter in the condensate is continuously separated and gas-lifted. The gaseous substances obtained by gas lifting are blocked by the baffle plate and return to the primary condensation unit, and exit the separation device through the gas outlet. The remaining condensate flows to the secondary condensation unit and is discharged from the separation device from the liquid outlet at the bottom of the secondary condensation unit.

[0046] To enable those skilled in the art to more clearly understand the present invention, the following embodiments will be used to provide a detailed description of a product separation method and apparatus for preparing olefins from syngas or CO2.

[0047] Example 1

[0048] The components are arranged as follows: primary condenser unit 1, variable diameter unit 2, packing unit 3 (80% porosity), secondary condenser unit 4, partition baffle 5, first heat exchanger 6, second heat exchanger 7, first product gas inlet pipe 8, second product gas inlet pipe 9, gas outlet 10, and liquid outlet 11. Figure 1 The structural diagram shown is assembled and connected to form a whole. The lower end of the first product gas inlet pipe 8 is close to the bottom of the first-stage condensation unit 1; the lower end of the second product gas inlet pipe 9 is inserted into the middle of the packing unit 3; the lower end of the partition baffle 5 is located at the middle position between the lower ends of the first product gas inlet pipe 8 and the second product gas inlet pipe 9.

[0049] Cooling water is introduced into the first heat exchanger 6 and the second heat exchanger 7 respectively to control the temperature of the first-stage condensing unit at 50℃ and the temperature of the second-stage condensing unit at 0℃.

[0050] The product gases for olefin preparation (200℃, composition: 30% H2O, 3% CO, 3% H2, 20% CO2, remainder C1-C) are respectively introduced into the first product gas feed pipe 8 and the second product gas 9. 20 The amount of product gas passing through the first product gas inlet pipe 8 is 10 times the amount of product gas passing through the inlet pipe 9. The product gas is cooled in the first-stage condensation unit 1, and the resulting large amount of condensate enters the packing unit 3 through the diameter-reducing unit 2.

[0051] The temperature of the cylinder wall of the packing unit 3 is affected by the low temperature of the second condensing unit 4, and the temperature decreases, which lowers the temperature of the liquid coming from the first condensing unit. This liquid then comes into contact with the product gas introduced into the second product gas feed pipe 9, forming a distillation process.

[0052] The distillation process continuously strips easily liquefiable organic compounds from the condensate, returning them to the primary condensation unit where they merge with all the gases. The gases then exit the separation unit from the right side of baffle 5 via gas outlet 10. This process can remove C4-C... 10 The component removal rate from water exceeds 97%. (C) 11 -C 20 The removal rate from water exceeds 70%.

[0053] The remaining condensate (mainly water) in packing unit 3 flows downwards naturally into secondary condensation unit 4. It is periodically discharged from liquid outlet 11.

[0054] Example 2

[0055] The components are arranged as follows: primary condenser unit 1, variable diameter unit 2, packing unit 3 (95% porosity), secondary condenser unit 4, partition baffle 5, first heat exchanger 6, second heat exchanger 7, first product gas inlet pipe 8, second product gas inlet pipe 9, gas outlet 10, and liquid outlet 11. Figure 1 The structural diagram shown is assembled and connected to form a whole. The lower end of the first product gas inlet pipe 8 is close to the bottom of the first-stage condensation unit 1; the lower end of the second product gas inlet pipe 9 is inserted into the middle of the packing unit 3; the lower end of the partition baffle 5 is located at the middle position between the lower ends of the first product gas inlet pipe 8 and the lower ends of the second product gas inlet pipe 9.

[0056] Cooling water is introduced into the first heat exchanger 6 and the second heat exchanger 7 respectively to control the temperature of the first-stage condensing unit at 85℃ and the temperature of the second-stage condensing unit at 25℃.

[0057] The product gases for olefin preparation (200℃, composition: 30% H2O, 3% CO, 3% H2, 30% CO2, remainder C1-C7) are introduced into the first product gas feed pipe 8 and the second product gas 9, respectively. The amount of product gas passing through the first product gas feed pipe 8 is 10 times the amount of product gas passing through the feed pipe 9. The product gases are cooled in the primary condensation unit 1, and the resulting large amount of condensate enters the packing unit 3 through the variable diameter unit 2.

[0058] The temperature of the cylinder wall of the packing unit 3 is affected by the low temperature of the second condensing unit 4, and the temperature decreases, which lowers the temperature of the liquid coming from the first condensing unit. This liquid then comes into contact with the product gas introduced into the second product gas feed pipe 9, forming a distillation process.

[0059] The distillation process continuously strips easily liquefiable organic compounds from the condensate and returns them to the primary condensation unit, where they merge with all the gases. The gases then exit the separation unit from the right side of baffle 5 via gas outlet 10. This process can remove over 95% of C4-C7 components from the condensate.

[0060] The remaining condensate (mainly water) in the packing unit 3 flows downward naturally into the secondary condensation unit 4 and is periodically discharged from the liquid outlet 11.

[0061] Example 3

[0062] The components are arranged as follows: primary condenser unit 1, variable diameter unit 2, packing unit 3 (90% porosity), secondary condenser unit 4, partition baffle 5, first heat exchanger 6, second heat exchanger 7, first product gas inlet pipe 8, second product gas inlet pipe 9, gas outlet 10, and liquid outlet 11. Figure 1 The structural diagram shown is assembled and connected to form a whole. The lower end of the first product gas inlet pipe 8 is close to the bottom of the first-stage condensation unit 1; the lower end of the second product gas inlet pipe 9 is inserted into the middle of the packing unit 3; the lower end of the partition baffle 5 is located at the middle position between the lower ends of the first product gas inlet pipe 8 and the lower ends of the second product gas inlet pipe 9.

[0063] Cooling water is introduced into the first heat exchanger 6 and the second heat exchanger 7 respectively to control the temperature of the first-stage condensing unit at 75℃ and the temperature of the second-stage condensing unit at 15℃.

[0064] The product gases for olefin preparation (at 200°C, composition: 18% H₂O, 10% CO, 10% H₂, 35% CO₂, remainder being C₁-C₂) are respectively introduced into the first product gas feed pipe 8 and the second product gas 9. 15 The amount of product gas passing through the first product gas inlet pipe 8 is five times the amount of product gas passing through the inlet pipe 9. The product gas is cooled in the first-stage condensation unit 1, and the resulting large amount of condensate enters the packing unit 3 through the reducing unit 2.

[0065] The temperature of the cylinder wall of the packing unit 3 is affected by the low temperature of the second condensing unit 4, and the temperature decreases, which lowers the temperature of the liquid coming from the first condensing unit. This liquid then comes into contact with the product gas introduced into the second product gas feed pipe 9, forming a distillation process.

[0066] The distillation process continuously strips easily liquefiable organic compounds from the condensate, returning them to the primary condensation unit where they merge with all the gases. The gases then exit the separation unit from the right side of baffle 5 via gas outlet 10. This process can remove C4-C... 10 The removal rate of components from the condensate exceeds 90%, C 11 -C 15 The removal rate of components from the condensate exceeds 85%.

[0067] The remaining condensate (mainly water) in the packing unit 3 flows downward naturally into the secondary condensation unit 4 and is periodically discharged from the liquid outlet 11.

[0068] Example 4

[0069] The components are arranged as follows: primary condenser unit 1, variable diameter unit 2, packing unit 3 (porosity 83%), secondary condenser unit 4, partition baffle 5, first heat exchanger 6, second heat exchanger 7, first product gas inlet pipe 8, second product gas inlet pipe 9, gas outlet 10, and liquid outlet 11. Figure 1 The structural diagram shown is assembled and connected to form a whole. The lower end of the first product gas inlet pipe 8 is close to the bottom of the first-stage condensation unit 1; the lower end of the second product gas inlet pipe 9 is inserted into the middle of the packing unit 3; the lower end of the partition baffle 5 is located at the middle position between the lower ends of the first product gas inlet pipe 8 and the lower ends of the second product gas inlet pipe 9.

[0070] Cooling water is introduced into the first heat exchanger 6 and the second heat exchanger 7 respectively to control the temperature of the first-stage condensing unit at 65℃ and the temperature of the second-stage condensing unit at 5℃.

[0071] The first product gas feed pipe 8 and the second product gas 9 are respectively introduced into the synthesis gas for olefin preparation (350℃, composition: 30% H2O, 3% CO, 3% H2, 40% CO2, the remainder being C1-C). 12 The amount of product gas passing through the first product gas inlet pipe 8 is four times the amount of product gas passing through the inlet pipe 9. The product gas is cooled in the first-stage condensation unit 1, and the resulting large amount of condensate enters the packing unit 3 through the reducing unit 2.

[0072] The temperature of the cylinder wall of the packing unit 3 is affected by the low temperature of the second condensing unit 4, and the temperature decreases, which lowers the temperature of the liquid coming from the first condensing unit. This liquid then comes into contact with the product gas introduced into the second product gas feed pipe 9, forming a distillation process.

[0073] The distillation process continuously strips easily liquefiable organic compounds from the condensate, returning them to the primary condensation unit where they merge with all the gases. The gases then exit the separation unit from the right side of baffle 5 via gas outlet 10. This process can remove C4-C... 10 The component removal rate from the condensate exceeds 93%. (C) 11 -C 12 The removal rate from condensate exceeds 70%.

[0074] The remaining condensate (mainly water) in the packing unit 3 flows downward naturally into the secondary condensation unit 4 and is periodically discharged from the liquid outlet 11.

[0075] Example 5

[0076] The components are arranged as follows: primary condenser unit 1, variable diameter unit 2, packing unit 3 (porosity 84%), secondary condenser unit 4, partition baffle 5, first heat exchanger 6, second heat exchanger 7, first product gas inlet pipe 8, second product gas inlet pipe 9, gas outlet 10, and liquid outlet 11. Figure 1The structural diagram shown is assembled and connected to form a whole. The lower end of the first product gas inlet pipe 8 is close to the bottom of the first-stage condensation unit 1; the lower end of the second product gas inlet pipe 9 is inserted into the middle of the packing unit 3; the lower end of the partition baffle 5 is located at the middle position between the lower ends of the first product gas inlet pipe 8 and the lower ends of the second product gas inlet pipe 9.

[0077] Cooling water is introduced into the first heat exchanger 6 and the second heat exchanger 7 respectively to control the temperature of the first-stage condensing unit at 65℃ and the temperature of the second-stage condensing unit at 10℃.

[0078] The first product gas feed pipe 8 and the second product gas 9 are respectively introduced into the synthesis gas for olefin preparation (280℃, composition: 25% H2O, 4% CO, 8% H2, 45% CO2, the remainder being C1-C). 14 The amount of product gas passing through the first product gas inlet pipe 8 is seven times the amount of product gas passing through the second product gas inlet pipe 9. The product gas is cooled in the first-stage condensation unit 1, and the resulting large amount of condensate enters the packing unit 3 through the diameter-reducing unit 2.

[0079] The temperature of the cylinder wall of the packing unit 3 is affected by the low temperature of the second condensing unit 4, and the temperature decreases, which lowers the temperature of the liquid coming from the first condensing unit. This liquid then comes into contact with the product gas introduced into the second product gas feed pipe 9, forming a distillation process.

[0080] The distillation process continuously strips easily liquefiable organic compounds from the condensate, returning them to the primary condensation unit where they merge with all the gases. The gases then exit the separation unit from the right side of baffle 5 via gas outlet 10. This process can remove C4-C... 10 The component removal rate from the condensate exceeds 92%. (The last part, "C," appears to be an unrelated fragment and is left untranslated.) 11 -C 14 The removal rate from condensate exceeds 78%.

[0081] The remaining condensate (mainly water) in the packing unit 3 flows downward naturally into the secondary condensation unit 4 and is periodically discharged from the liquid outlet 11.

[0082] Example 6

[0083] The components are arranged as follows: primary condenser unit 1, variable diameter unit 2, packing unit 3 (91% porosity), secondary condenser unit 4, partition baffle 5, first heat exchanger 6, second heat exchanger 7, first product gas inlet pipe 8, second product gas inlet pipe 9, gas outlet 10, and liquid outlet 11. Figure 1The structural diagram shown is assembled and connected to form a whole. The lower end of the first product gas inlet pipe 8 is close to the bottom of the first-stage condensation unit 1; the lower end of the second product gas inlet pipe 9 is inserted into the middle of the packing unit 3; the lower end of the partition baffle 5 is located at the middle position between the lower ends of the first product gas inlet pipe 8 and the lower ends of the second product gas inlet pipe 9.

[0084] Cooling water is introduced into the first heat exchanger 6 and the second heat exchanger 7 respectively to control the temperature of the first-stage condensing unit at 55℃ and the temperature of the second-stage condensing unit at 3℃.

[0085] The olefin production product gases (200℃, composition: 15% H2O, 30% CO, 30% H2, 25% CO2, and the remainder C1-C8) are introduced into the first product gas feed pipe 8 and the second product gas feed pipe 9, respectively. The amount of product gas passing through the first product gas feed pipe 8 is six times the amount of product gas passing through the second product gas feed pipe 9. The product gases are cooled in the primary condensation unit 1, and the resulting large amount of condensate enters the packing unit 3 through the variable diameter unit 2.

[0086] The temperature of the cylinder wall of the packing unit 3 is affected by the low temperature of the second condensing unit 4, and the temperature decreases, which lowers the temperature of the liquid coming from the first condensing unit. This liquid then comes into contact with the product gas introduced into the second product gas feed pipe 9, forming a distillation process.

[0087] The distillation process continuously strips easily liquefiable organic compounds from the condensate and returns them to the primary condensation unit, where they merge with all the gases. The gases then exit the separation unit from the right side of baffle 5 via gas outlet 10. This process can remove over 90% of C4-C8 components from the condensate.

[0088] The remaining condensate (mainly water) in the packing unit 3 flows downward naturally into the secondary condensation unit 4 and is periodically discharged from the liquid outlet 11.

[0089] Example 7

[0090] The components are arranged as follows: primary condenser unit 1, variable diameter unit 2, packing unit 3 (92% porosity), secondary condenser unit 4, partition baffle 5, first heat exchanger 6, second heat exchanger 7, first product gas inlet pipe 8, second product gas inlet pipe 9, gas outlet 10, and liquid outlet 11. Figure 1 The structural diagram shown is assembled and connected to form a whole. The lower end of the first product gas inlet pipe 8 is close to the bottom of the first-stage condensation unit 1; the lower end of the second product gas inlet pipe 9 is inserted into the middle of the packing unit 3; the lower end of the partition baffle 5 is located at the middle position between the lower ends of the first product gas inlet pipe 8 and the lower ends of the second product gas inlet pipe 9.

[0091] Cooling water is introduced into the first heat exchanger 6 and the second heat exchanger 7 respectively to control the temperature of the first-stage condensing unit at 60℃ and the temperature of the second-stage condensing unit at 15℃.

[0092] The product gases for olefin preparation (300℃, composition: 18% H2O, 10% CO, 15% H2, 60% CO2, remainder C1-C) are introduced into the first product gas feed pipe 8 and the second product gas 9, respectively. 12 The amount of product gas passing through the first product gas inlet pipe 8 is six times the amount of product gas passing through the second product gas inlet pipe 9. The product gas is cooled in the first-stage condensation unit 1, and the resulting large amount of condensate enters the packing unit 3 through the reducing unit 2.

[0093] The temperature of the cylinder wall of the packing unit 3 is affected by the low temperature of the second condensing unit 4, and the temperature decreases, which lowers the temperature of the liquid coming from the first condensing unit. This liquid then comes into contact with the product gas introduced into the second product gas feed pipe 9, forming a distillation process.

[0094] The distillation process continuously strips easily liquefiable organic compounds from the condensate, returning them to the primary condensation unit where they merge with all the gases. The gases then exit the separation unit from the right side of baffle 5 via gas outlet 10. This process can remove C4-C... 10 The component removal rate from the condensate exceeds 94.5%, and C 11 -C 12 The removal rate of components from the condensate exceeds 79%.

[0095] The remaining condensate (mainly water) in the packing unit 3 flows downward naturally into the secondary condensation unit 4 and is periodically discharged from the liquid outlet 11.

[0096] Example 8

[0097] The components are arranged as follows: primary condenser unit 1, variable diameter unit 2, packing unit 3 (porosity 85%), secondary condenser unit 4, partition baffle 5, first heat exchanger 6, second heat exchanger 7, first product gas inlet pipe 8, second product gas inlet pipe 9, gas outlet 10, and liquid outlet 11. Figure 1 The structural diagram shown is assembled and connected to form a whole. The lower end of the first product gas inlet pipe 8 is close to the bottom of the first-stage condensation unit 1; the lower end of the second product gas inlet pipe 9 is inserted into the middle of the packing unit 3; the lower end of the partition baffle 5 is located at the middle position between the lower ends of the first product gas inlet pipe 8 and the lower ends of the second product gas inlet pipe 9.

[0098] Cooling water is introduced into the first heat exchanger 6 and the second heat exchanger 7 respectively to control the temperature of the first-stage condensing unit at 52℃ and the temperature of the second-stage condensing unit at 13℃.

[0099] The olefin production product gases (100℃, composition: 17% H2O, 20% CO, 30% H2, 32% CO2, and the remainder C1-C6) are introduced into the first product gas feed pipe 8 and the second product gas feed pipe 9, respectively. The amount of product gas passing through the first product gas feed pipe 8 is three times the amount of product gas passing through the second product gas feed pipe 9. The product gases are cooled in the primary condensation unit 1, and the resulting large amount of condensate enters the packing unit 3 through the variable diameter unit 2.

[0100] The temperature of the cylinder wall of the packing unit 3 is affected by the low temperature of the second condensing unit 4, and the temperature decreases, which lowers the temperature of the liquid coming from the first condensing unit. This liquid then comes into contact with the product gas introduced into the second product gas feed pipe 9, forming a distillation process.

[0101] The distillation process continuously strips easily liquefiable organic compounds from the condensate and returns them to the primary condensation unit, where they merge with all the gases. The gases then exit the separation unit from the right side of baffle 5 via gas outlet 10. This process can remove over 91% of C4-C6 components from the condensate.

[0102] The remaining condensate (mainly water) in the packing unit 3 flows downward naturally into the secondary condensation unit 4 and is periodically discharged from the liquid outlet 11.

[0103] Example 9

[0104] The components are arranged as follows: primary condenser unit 1, variable diameter unit 2, packing unit 3 (porosity 88%), secondary condenser unit 4, partition baffle 5, first heat exchanger 6, second heat exchanger 7, first product gas inlet pipe 8, second product gas inlet pipe 9, gas outlet 10, and liquid outlet 11. Figure 1 The structural diagram shown is assembled and connected to form a whole. The lower end of the first product gas inlet pipe 8 is close to the bottom of the first-stage condensation unit 1; the lower end of the second product gas inlet pipe 9 is inserted into the middle of the packing unit 3; the lower end of the partition baffle 5 is located at the middle position between the lower ends of the first product gas inlet pipe 8 and the lower ends of the second product gas inlet pipe 9.

[0105] Cooling water is introduced into the first heat exchanger 6 and the second heat exchanger 7 respectively to control the temperature of the first-stage condensing unit at 75℃ and the temperature of the second-stage condensing unit at 25℃.

[0106] The product gases for olefin preparation (at 150°C, composition: 10% H₂O, 15% CO, 20% H₂, 45% CO₂, remainder being C₁-C₂) are introduced into the first product gas feed pipe 8 and the second product gas 9, respectively. 20The amount of product gas passing through the first product gas inlet pipe 8 is 10 times the amount of product gas passing through the second product gas inlet pipe 9. The product gas is cooled in the first-stage condensation unit 1, and the resulting large amount of condensate enters the packing unit 3 through the diameter-changing unit 2.

[0107] The temperature of the cylinder wall of the packing unit 3 is affected by the low temperature of the second condensing unit 4, and the temperature decreases, which lowers the temperature of the liquid coming from the first condensing unit. This liquid then comes into contact with the product gas introduced into the second product gas feed pipe 9, forming a distillation process.

[0108] The distillation process continuously strips easily liquefiable organic compounds from the condensate, returning them to the primary condensation unit where they merge with all the gases. The gases then exit the separation unit from the right side of baffle 5 via gas outlet 10. This process can remove C4-C... 10 The component removal rate from the condensate exceeds 92%, C 11 -C 20 The removal rate from condensate exceeds 72%.

[0109] The remaining condensate (mainly water) in the packing unit 3 flows downward naturally into the secondary condensation unit 4 and is periodically discharged from the liquid outlet 11.

[0110] In the description of this specification, the references to terms such as "one embodiment," "some embodiments," "example," "specific example," or "some examples," etc., indicate that a specific feature, structure, material, or characteristic described in connection with that embodiment or example is included in at least one embodiment or example of the invention. In this specification, the illustrative expressions of the above terms do not necessarily refer to the same embodiment or example. Furthermore, the specific features, structures, materials, or characteristics described may be combined in any suitable manner in one or more embodiments or examples. In addition, those skilled in the art can combine and integrate the different embodiments or examples described in this specification.

[0111] For the sake of simplicity, the method embodiments are described as a series of actions. However, those skilled in the art should understand that the present invention is not limited to the described order of actions, as some steps can be performed in other orders or simultaneously according to the present invention. Furthermore, those skilled in the art should also understand that the embodiments described in the specification are preferred embodiments, and the actions and components involved are not necessarily essential to the present invention.

[0112] The above provides a detailed description of a product separation method and apparatus for preparing olefins from syngas or CO2 provided by the present invention. Specific examples have been used to illustrate the principle and implementation of the present invention. The description of the above embodiments is only for the purpose of helping to understand the method and core idea of ​​the present invention. At the same time, for those skilled in the art, there will be changes in the specific implementation and application scope based on the idea of ​​the present invention. Therefore, the content of this specification should not be construed as a limitation of the present invention.

Claims

1. A product separation device for the preparation of olefins from syngas or CO2, characterized in that, The device includes a primary condensation unit, a variable diameter unit, and a packing unit connected in sequence, as well as a secondary condensation unit surrounding the packing unit. The primary condensation unit includes a first product gas inlet pipe, a second product gas inlet pipe, and a partition baffle; wherein, the lower end of the first product gas inlet pipe is located in the primary condensation unit, the lower end of the second product gas inlet pipe is located in the packing unit, and the lower end of the partition baffle is located in the area between the lower ends of the first product gas inlet pipe and the lower ends of the second product gas inlet pipe, and the first product gas inlet pipe and the second product gas inlet pipe are both located on the same side of the partition baffle; The bottom of the secondary condensation unit is provided with a liquid outlet for receiving the remaining condensate flowing out of the packing unit and discharging it from the separation device. The top of the primary condensation unit is also provided with a gas outlet, which is located on the other side of the partition baffle.

2. The product separation device for olefin production from syngas or CO2 according to claim 1, characterized in that, The primary condensation unit controls the temperature of the condensation zone to be between 50-85 ℃ by setting a first heat exchanger; The secondary condensation unit controls the temperature of the condensation zone between 0 and 25 °C by setting a second heat exchanger.

3. The product separation device for olefin production from syngas or CO2 according to claim 2, characterized in that, The primary condensing unit and the secondary condensing unit achieve temperature control through cooling water circulation.

4. The product separation device for olefin production from syngas or CO2 according to claim 1, characterized in that, The porosity of the packing unit is 80%-95%.

5. The product separation device for olefin production from syngas or CO2 according to claim 1, characterized in that, The amount of product gas introduced into the first product gas inlet pipe is 2-10 times that of the second product gas inlet pipe.

6. A method for separating products from olefins prepared from syngas or CO2, characterized in that, The method is applicable to the product separation apparatus for olefin production from syngas or CO2 as described in any one of claims 1-5, and the method includes the following steps: Step 1: Control the condensation zone temperature of the primary condensation unit to 50-85 ℃, and control the condensation zone temperature of the secondary condensation unit to 0-25 ℃; Step 2: Product gas with a volume ratio of 2-10:1 is introduced into the first product gas inlet pipe and the second product gas inlet pipe respectively. The product gas introduced into the first product gas inlet pipe is condensed in the first-stage condensation unit to form condensate liquid. The condensate liquid enters the packing unit through the diameter reducing unit. Step 3: The temperature of the packing unit's cylinder wall is affected by the low temperature of the secondary condensation unit, and the temperature of the condensate entering it becomes even lower. It comes into contact with the product gas introduced through the second product gas feed pipe, and under the action of the temperature difference, the easily liquefied organic components in the condensate are continuously stripped by the gas. The gaseous substances obtained by the gas stripping are blocked by the baffle plate and return to the primary condensation unit, and exit the separation device through the gas outlet. The remaining condensate flows to the secondary condensation unit and is discharged from the separation device from the liquid outlet at the bottom of the secondary condensation unit. The product gases include CO, H2, CO2, and Cl-C. 20 Organic matter; The temperature of the product gas is 100-350 ℃.

7. The product separation method according to claim 6, characterized in that, In step 1, controlling the condensation zone temperature of the primary condensing unit to be 50-85 ℃ includes: introducing circulating cooling water into the first heat exchanger to control the condensation zone temperature of the primary condensing unit to be 50-85 ℃. Controlling the condensation zone temperature of the secondary condensing unit to 0-25 ℃ includes: introducing circulating cooling water into the second heat exchanger to control the condensation zone temperature of the secondary condensing unit to 0-25 ℃.

8. The product separation method according to claim 6, characterized in that, The packing unit is a plastic packing unit, a metal wire mesh packing unit, or a ceramic packing unit, with a porosity of 80%-95%.

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